Process of continuously distilling carbonaceous fuel



June 26, 1928. I w. E. TRENT PROCESS OF CONTINUOUSLY DISTILLING CARBONACEOUS FUEL Filed Dec. 22, 1922 um/atom Mic/2. 5mi

h u n L June 26, 1928.

W. E. TRENT PROCESS OF CONTINUOUSLY DISTILLING CARBONACEOUS FUEL Filed Dec. 22. 1922 s Sheets-Sheet 2 June 26, 1928. 1,675,315

W. E. TRENT PROCESS OF CONTINUOUSLY DISTILLING CARBONAGEOUS FUEL Filed Dec. 22, 1922 3 Sheets-Sheet 3 $5 Wallerl ffi'eni Patented June 26, 1928.

UNITED STATES PATENT OFFICE.

WALTER EDWIN TRENT, OF WASHINGTON, DISTRICT OF COLUMBIA, ASSIGNOR TO TRENT PROCESS CORPORATION, OF NEW YORK, N. Y., A CORPORATION OF DELA- WARE.

PROCESS OF CONTINUOUSLY DISTILLING CARBONAOEOUS FUEL.

Application filed December 22, 1922. Serial No. 608,530.

The invention relates to improvements in the art of distilling coals, lignites and the like.

The invention broadly comprehends the distillation of coals for the manufacture of carbonaceous products with an independent fractional collection of the various condensa-ble oils distilled from the coal.

It is a primary object of the invention to provide a process for distilling coals for the production of coke and the recovery of the volatiles in said coals, by which process substantially all of the heat of the hot gases is utilized in the distillation of the coals, the volatiles vaporized by such heat being separately collected as a plurality of different fractions according to the boiling points thereof.

With the"foregoing conception in mind, the invention more specifically constitutes a process for the continuous distillation of coal, or coal and oil mixtures, wherein the carbonaceous fuel is placed within a series of containers separated by oil traps that receive different condensed fractions removed from the coal. Heating gases of combustion are applied to the coal in one of said containers, and these gases then pass successively through charged containers before they are permitted to discharge. The material in the container through which the gases first pass is thus subjected to the maximum temperature of the gases, which treatment is maintained until the volatiles have been removed from the material in said container and a coke or carbonized residue formed. The heating gases from this container continuously pass through coal in the succeeding containers. The temperature of said gases drops a substantial degree after passa e through each container whereby substantial ly all the heat of the gases is utilized prior to discharge thereof. The drop intemperature in each container results in the vaporization of the different fractions of the "01- atile products contained in the coal, and these fractions separately condensed are re-.

coveredas different fractions. Oils vaporizing from the fuel in one container having a certain boiling point are largely condensed bypassage through the container of the next succeeding lower temperature, and

it and the other the fractions thus condensed in each contamer are separately collected. This operation continues during the passage of the gases through the various containers resulting in the collection of the various condensable products as fractions according to. their boiling points. When the material in one container in the series'has been sufiiciently treated to produce coke, then the maximum temperature due to the combustion of gases is imparted to the next succeeding container, the lower boiling point hydrocarbon materials in which have been previously removed by vaporization because of the passage of heating gases therethrough. The condensed oils collecting in the various receivers or traps interposed between the containers are separately discharged so that the different condensable fractions of the oil contained in the hydrocarbon material are separately and independently collected.

In the accompanying drawings I have disclosed a single embodiment of an apparatus capable of supporting this process, but this disclosure is merely made for the purpose of illustration and may be regarded as illustrative only of many others.-

In the drawings:

Figure 1 represents a top plan view of a battery of the containers as they are positioned; i v

Figure 2 is a longitudinal view in vertical section with arts broken away;

Figure 3 1s a vertical sectional view through a pair of opposite coking containers; and I Figure 4 represents a single container with the lifting device in operative relation thereto.

Referring now more particularly to the drawings wherein like reference characters indicate corresponding parts, the numerals 1, 2, 3, 4, 5, 6, 7, 8, 9 and 10 designate a se-w er metallic shell 12, having a removable closure 12*, lined with a suitable lining of silica or the like 12', and provided with a water seal 12 between the wall of the container 12 and said closure. Each container is, furthermore, provided with, outstanding lugs 12 adapted to be en aged by a grapple 13 operated by means 03? an overhead crane or the like, whereby the containers may be lifted and transported from one position to another, which is necessary during the operation of the process. These containers may be of any configuration, but I have shown them as of a circular form, although it is apparent that they may be rectangular, if desired. Each container or part 12 is constructed slightly larger in diameter at the top than at the bottom thereof,-so as to retain the charge therein when coked or carbonized, and to facilitate the emptying of the charge, which charge is indicated by the reference character 14, having formed therein a. plurality of vertical passageways 15 to permit the free passage of heating gases through the charge as shown bykthe arrows A in Figure 3.

The fuel charge placed in the shells 12 in the containers 1, 2, 3, 4, 5, 6, 7, 8, 9 and 10 may be of any desired composition, but prefera ly consists of amalgamated masses of fine coal particles and oil 'of a plastic consistenc resembling putty, mortar, or the like. uch a plastic mass is readily capable of being formed into the molded charges disclosed in the drawings, and, furthermore, a mixture of fine coal and oil has been found to be highly efficient in the production of domestic, industrial, and metallurgical cokes. In my Patent No. 1,420,164, I have disclosed and claimed a process for manufacturing this material, and while it will be understood that this material is most efiicient for use in the present process, the process is not, however, limited to the employment of such fuel.

The various pots or containers 1 to 10 inclusive, hereinbefore mentioned, are each preferably seated on a refractory base 16, composed of any suitable heat resisting material, such as silica, fire brick, etc. Each base is formed with a perforated container charge in each of the containers so as to permit a free circulation of gases through said openings in the charges in a manner which will more fully hereinafter appear.

The container bases 16 are preferably arranged in parallel lines, in the present illustration five being disposed in "each line.

, This, of course, means that five containers are likewise positioned on their respective bases, and the containers form two parallel rows. The containers 1 to 10 inclusive, and the bases 16 therefor, all communicate with the continuous flue 17, which consists of two parallel side portions extending respectively beneath the two lines of container bases and end portions 17 joining the parallel side portions and thereby formin a continuous endless flue. Interposed in this flue 17 are a plurality of baflles, being designated by the reference characters 1,-2, 3, 4, 5, 6, 7, 8, 9' and 10, there being one battle for each container retort, which baflles serve to cause the heating gases to travel upwardly and then downwardly through the openings in each. charge. There is also provided within the flue 17 a series of oil traps 1*, 2, 3*, 4 5 6, 7, 8, 9, 10, one oil trap being dispose beneath each of the containers having the carbonaceous charge. These oil traps are divided into two compartments by reason of the baflles 1 to 10, inclusive, the baflie 1' dividing the oil pot 1, while the other oil pots are similarly divided by the other baffies. The two compartments of each baflle are provided with separate draw off-pipes or lines 19 and 19, each of said lines having manually controlled valves 20 therein for controlling the passage of oil, and at the same time preventing the escape of combustible gases during certain operations.

Leading to the flue 17 I provide a plurality of gas burners 1, 2", 3 4 5 6 7 8", 9", and 10", the gas burner 1 being, of course, located in the retortbeneath the pot 1, while the burner 2 is beneath the retort supporting the pot 2, etc. These gas burners 1 to 1O inclusive, are fed by means of a feed pipe 21, and independent valves 22 control each burner, so that one burner can be used to the exclusion of the others. One of the burners is shown in detail in Figure 2 as entering the flue 17 and positioned directly beneath one of the pots. While I have herein shown gas burners as heating means for said pots, it will be distinctly understood that other types of heaters may be employed, ls iich, for instance, as electric heaters or the Disposed between the two rows of containers 1 to 10 inclusive, and communicating with the flue 17, I provide a discharge flue 24, having branches 25 leading from the fine 17 at a point beneath each of the containers 1 to 10 inclusive. Said branches 25 are preferably provided with manually controlled gate valves 26, the valve in each branch being operable independently of the valves in the other branches, for the purpose of opening or closing the communication between the flue 17 and any one of the branches.

' the gases passing therethrough being permitted to escape. I

Reverting now to the flue 17 and its con nections 17-, there is disposed in this fine a series of slide valves 1, 2, 3, 4, 5 6, 7, 8, 9, 10, one of the valves being positioned intermediate each two adjacent containers, except that between. the end containers 3 and 4, and 8 and 9, respectively, two of such valves are used as shown, and being so arranged as to control the passage of the heating gases througlrside portions of the flue 17 and its connecting end portions 17, whereby said gases are caused to pass successively through the material in the different containers and impart their heat thereto before they are permitted to escape, and to prevent said gases from recirculating through the system.

In carrying the process into actual use, I generally employ eight of the containers at a time, two additional containers being used in the system to permit the loading and unloading of said containers during the continuous operation of the plant. Assumingthat containers 1 to 8-inclusive, are in use and positioned on the retort supports 16 with all the containers filled with green fuel, I then light the gas burner 8", under the container 8 and the charge in this container is then subjected to a maximum temperature and is converted into coke, while the condensable oils are vaporized and non-condensable gases formed.

This container 8 is preferably subjected to a temperature of approximately 1600 F. The heat causes a rapid carbonization' of the fuel mass therein, and. the vaporized oils and gases, together with the heated products of combustion, pass outwardly and downwardly from the container 8 into the fine 17. As the gases and vapors leave the container 8, they pass at a lower temperature on through the flue 17 until they encounter the bafile 7' be neath the container 7, and here the vaporized products and the exhaust products of combustion pass through the openings in the fuel charge in this container 7 in an upward and then downward direction, asshown by the arrows A. The temperatureof these gases is sufiicient to vaporize certain constituents within the fuel mass inthe container 7, although they are decidedly lower in temperature than when they first pass from the container 8. This lowering in temperature in the second container 7, because of contact of the gases with the green fuel and loss by heat radiation, results in a condensing of certain heavier fractions of high boiling points which were vaporized from the material in the container 8, and these condensed fractions, such as heavier tars, pitches, etc., flow into, and are collected, in the two'compartments of the oil pot 7, being withdrawn therefrom, through the drawout lines 19 and 19. The vaporized fractionsof lower boi1- ing points, which are removed from the fuel in the container 8 and also in the container 7 do not condense at the temperatures maintained in these two containers, but pass on with the exhaust gases into the next succeeding container in the series designated by the character 6. Thereis, of course, a drop in temperature in this container of say from 100 to 200 F. by reason of heat losses and from contact with the materials encountered, and naturally during the passage of such products through said container 6, the heavier fractions,.or those condensable vapors which have the higher boiling points, are condensed and largely collected in the compartments of the oil pot 6. Manifestly, the oils collected in the oil pots 6 and 7 are radically different in boiling points, and it will thus be seen that the oils produced by the distillation are independently collected and represent different fractions'approximately separated according to their boiling points. The exhaust gases and vapors from the container 6 pass on then through the flue 17 into the next succeeding containerifi, these gases being sufliciently hot to remove certain volatiles from the material in this container, while the next highest cut in the condensable gas content of said gases will be condensed, and the oil collected in the compartments of the oil pot 5. This operation is continued until the exhaust gases and certain condensable and uncondensable gases have passed successively through the carbonaceous fuel inthe containers 4, 3, 2 and 1, it being understood that during this operation gaseous fuel is being burned only beneath the container 8 while reducing the material therein to coke. The heating gases passing from this container, however, have been robbed of most of their heat, so that this heat is utilized to the greatest possible extent before the gases are permitted finally to discharge, and these gases during their passage serve to vaporize constituents having different boiling points in the successive pots, the condensable fractions being in turn condensed and collected in accordance with their boiling points as separate fractions in the various oil pots 8 to 1 inclusive. During this operation, the slide Valves 26 in the extensions have allbeen maintained in a closed position to prevent the discharge of the exhausted gases from the various pots into the discharge flue 24, save the valve 26 of the pot 1, this valve being open so as to permit the heating gases which at this time are at or near a temperature not exceeding the boiling point of water to pass on into the dischargeflue 24, where certain condensable vapors are separated from the exhaust gases, and the exhaust gases permitted to escape. It

will, furthermore, be understood that during the operation just described, all of the slide valves 1 to 10 n usive ar open, save the slide valve 10 between the cokin containers 1 and 10 and the slide valves 8 etween the containers 8 and 9. The slide valve 10, being closed, prevents a further passage of the gases which are to be shunted into the flue 24 when they have travelled through the container 1, while the slide valves 8 prevent a backward passage of h ating gases from the retort beneath the container 8, which container,in the present example, is the one that is being subjected to a maximum temperature.

During theoperation as above pointed out, the gases that discharge from the last container 1 are preferably at a very low temperature, so that practically all of the heat has been utilized in the removal of volatiles from the carbonaceous fuel in the successive containers, and the successive drops in temperatures in eachsucceeding container has resulted in a condensation of the condensable vapors in accordance with their boiling points, so that there has been a shar separation of the hydrocarbon oils into di ferent fractions of like boiling point. The

fractions are separately collected in the different oil traps or pots 1 to 8, inclusive, and the oil in these pots is drawn off separately through the discharge lines 19 and 19 as desired, it being apparent that in one pot there will be a substantial quantity of oil, such as, benzol, gasoline, or certain light ends, while in a preceding pot kerosene or similar oil will collect, the other pots containing oil of successively higher boiling points. When the fuel mass injhe container 8 has been converted to coke, heat is no longer applied to this container by means "of the burner 8", and the container 1s removed for the discharge of its coke, a green supply of fuel being placed therein. The-burner 7 is then preferably lighted beneath the container 7, the fuel in which has been partially carbonized because of being subjected to the heat of the gases issuing from the previous container 8. This container 7 is then subjected to the primary'heat, it being understood that the valve 7 between the containers Sand 7 has been closed, so that there will be no back passage of heating gases. The charge in the container 7, soon after being subjected to primary heat, is converted to coke, the gases, of course, assing on out through the successive containers 6, 5, 4, 3, 2, 1 and 10, which latter container has a green fuel charge and has just been placed in the circuit, to impart heat to the fuel in these containers to vaporize volatiles therein and partially 'carbonize the fuel, which is at the. same time causing a convdensation of different condensable vapors,

which fractions are separately caught in their respective oil traps or pots beneath each container in amanner as has been hereim before mo e ,fully de cribe W n t fu l charge in the container 7 has been coked or carbonized, then the fuel in the container 6, which has been partially coked because of its being subjected to the action of the hot gases that have previously passed from the containers 8 and 7, is subjected to primary heat by the lighting of the burner 6 thereunder,

and the material in this container is then' .circuit during the operation, and constituting unloading and charging containers. As the primary heat is advanced from one container to another, the slide valves 1 to 10 inclusive, and the slide valves 26 controlling the passage of exhaust gases to the stack 24 are properly controlled, which is clear from the description that has been hereto- .fore given. It may be again stated, however,

that the control of these valves is such that the valve disposed in the flue 17 immediatel behind the container being subjected to t e rimary heat is closed, while all of the other ue valves are 0 en save the flue valve immediately ahead of the last container in the series which serves to shunt the exhaust gases out through the single open valve 26 and into the'flue 24, it being" apparent that only one of the valves 26 is open at a single time, and this valve permits the discharge of gases from the last container in the series.

Instead of introducing heating gases to each container as the coke making advances from one pot to another, I may, when pot 8, for instance, has yielded its gas and the residue has become converted into coke, introduce steam through the combined air and steam feeding pi e 31 communicating with the independent eeds 30, one being disposed beneath each pot. When steam is introduced to quench the coke mass, the gases produced by reason of the decomposition of the coke steam, pass out through the appropriate flue by opening its valve 26 rather than successively through the series of communicating pots. Air may be introduced in a regulated uantity whereby combustion is controlled t rough this combined air and steam feed the grapple 13, which is suspended by a flexible member 31 carried by an overhead crane 32 which enables the pots to be freely lifted from their bases, discharged, refilled,

and then replaced.

'In carrying out the proceijs various temperatures may be resorted to, but I preferably use a maximum temperature of say from 1600 F. to 1800 F., which is the temperature of the heating gases as applied to the container having the coal which is being converted into coke and this temperature progressively drops as the gases pass through the succeeding fuel masses in the other containers so as to cause a fractional condensation of the condensable .vapors, which condensates are separately caught or collected in the various oil pots interposed between V the containers, and the exhaust gases are finally discharged when only slightly above an atmospheric temperature.

In the claims I employ the word coal to include any carbonaceous material which either consists of or is formed from a solid carbonaceous material having a hard carbonized outer surface.

Having thus described my invention, what I claim is:

1. The process of distilling coals to produce coke and to recover condensable oils in fractions, consisting in introducing to a series of coking containers carbonaceous fuel matter, in applying heat directly to the fuel in one of said containers sufficient to vaporize the volatile constituents thereof and to form a coke residue, in causing the exhaust gases 9f combustion and vaporized products rom said container to pass successively together through the series of containers whereby the material therein is subjected to heat of a progressively decreasing temperature to vaporize volatiles in the coal in said containers and to fractionally condense different condensable vapors passing through the containers, in separately collecting the different condensed fractions, in withdrawin the respective condensed fractions from eac 1 respective container, in removing a. coke mass from said first mentioned container, and in thereafter repeating said operations, successively applying a coking temperature to the succeeding partially treated containers.

2. The process of continuously distilling coals to produce coke and to recover condensable oils in fractions consisting in introducing to a series of coking containers carbonaceous fuel matter, in applying heat directly to the fuel in one of said containers sufficient to vaporize the volatile constituents thereof and to form a coke residue, in causing the exhaust gazes of combustion and vaporized products from said container to pass successively together through the series of containers whereby the material therein is subjected to a heat of a progressively decreasing temperature to vaporize volatiles in the coal in said con tainers and to fractionally condense different condensable vapors passing through the containers, in separately collecting the different condensed fractions, in withdrawing the respective condensed fractions from each respective .container, in removing a coke mass from said first mentioned container, and in thereafter repeating said operations, successively applying a coking temperature to the succeeding partially treated containers, and in replacing the coked mass removed from each container in turn with a green carbonaceous fuel charge to be treated in the series in its proper sequence.

3. The process of distilling comminuted coal to form a carbonized residue and to recover contained oils infractions according containers, each adapted to receive a comminuted carbonaceous fuel, in applying heat directly to one of said containers suflicient to remove the volatiles from the fuel mass therein and to form a carbonized residue, in causing the products of combustion and removed volatiles to pass from said container successively together through said succeeding containers communicating with one another, the temperature ofvsaid products of combustion and said vaporized constituents dropping during the passage thereof through such succeeding containers to vaporize different volatile constituents contained in the material in said containers, and to frac'tionally condense different travelling condensable vapors removed from said material when passing through the various containers, according to their @different boiling points, in separately collecting said condensable oils as independent fractions having diiferent'boiling points in withdrawing the respective condensed fractions from each respective container in removing said first mentioned container when the fuel mass therein has been carbonized, in thereafter successively applying the maximum heat to the carbonaceous masses in said succeeding containers to carbonize the fuel therein and recover the condensable'oils as separate fractions, and in replacing the carbonized masses with green fuel to be placed in communication with the other containers in their proper order to have the fuel therein subjected to the heating gases, and in finally discharging said exhaust gases after passage throu h the series of containers.

4 4. g rocess of distilling a plastic fuel compose of pulverized coal and oil, consisting in introducing said-fuel to a plurality of communicating containers arranged in series, in applying primary heat directly to the fuel in one of said containers sufficient to vaporize the volatiles therein and form a carbonized residue, in causing exhaust gases of combustion and vaporized products from said container to pass successively together through the series of the containers whereby the fuel therein is subjected to heat of progressivelydecre'asing temperature to vaporize volatiles in said succeeding containers and to simultaneously fractionally condense sisting in introducing said fuel to a plurality of communicating containers arranged in series, in applying primary heat directly to the fuel in one of said containers sufficient to va orize the volatiles therein and form a car onized residue, in causing exhaust gases and vaporized products from said container to pass successivelytogether through the series of the containers whereby the fuel therein is subjected to heat of progressively' decreasing temperature to vaporize volatiles in said succeeding containers and to simultaneousl' fractionally con densedifierent condensa le vapors passingthrough the containers, in separately collecting t e different condensed fractlons and withdrawing the respective condensed frac-' tlons from each respective container, 1n removing the carbonized mass from said first mentioned container, and in repeating said operations successively applying the primary heat tosucceeding containers of partially treated material.

6. A process for distilling a plastic fuel composed of pulverized coal and oil, consisting in introducing-a charge of said fuel having passageways formed therethrough to a plurality of containers arranged in series, in

of the passageways of the fuel in one of said chambers sufficient to vaporize the volatiles therein and form a carbonized residue, in causing exhaust gases of combustion and vaporized products from said container to pass successively together through the series of containers in contact with the walls of the passageways formed in the fuel masses therein whereby the said products are cooled and thereby condensed and the fuel in said succeeding containersis subjected to a progressively decreasing temperature, in collecting the condensates produced in the different containers, in -Withdrawing the respective condensed fractions produced by each respective container, and in repeating said operations advancing the primary heat to a succeeding container in the series whenthe fuel charge in the first mentioned containerhas been coked.

7. A process for distilling a plastic fuel composed of pulverized coal and oil, consisting in introducing a charge of said fuel having passageways formed therethrough to a plurality of containers arranged in series, in applying primary heat directly to the walls of the passageways of the fuel in one of said chambers sufficient to vaporize the volatiles therein and form a carbonized residue, in causing exhaust gases of combustion and vaporized applying primary heat directly to the Walls products from said container to pass successively together through the series of containers in contact with the walls of the passageways formed in the fuel masses therein whereby the said products are cooled and thereby condensed and the fuel in said succeeding containers is subjected to a progressively decreasing temperature, in collecting the condensates roduced in the different containers, in withdrawing the respective" condensed fractions produced by each respective container, in repeating said operations and advancing the primary heat to a suc- 100 ceeding container in the series when the fuel charge in the first mentioned container has .been coked, and in removing the carbonized coals from said first-mentioned container.

ture.

WALTER EDWIN TRENT.

In testimony whereof I aflix my signa- .105 

